WO2014097799A1 - Procédé d'hydrolyse d'une biomasse végétale - Google Patents

Procédé d'hydrolyse d'une biomasse végétale Download PDF

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Publication number
WO2014097799A1
WO2014097799A1 PCT/JP2013/081181 JP2013081181W WO2014097799A1 WO 2014097799 A1 WO2014097799 A1 WO 2014097799A1 JP 2013081181 W JP2013081181 W JP 2013081181W WO 2014097799 A1 WO2014097799 A1 WO 2014097799A1
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acid
plant biomass
reaction solution
reaction
equivalent concentration
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PCT/JP2013/081181
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English (en)
Japanese (ja)
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藤田　一郎
米田　正
福岡　淳
小林　広和
瑞帆 藪下
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昭和電工株式会社
国立大学法人北海道大学
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Priority to JP2014553028A priority Critical patent/JPWO2014097799A1/ja
Priority to US14/652,980 priority patent/US20150337401A1/en
Priority to BR112015014153A priority patent/BR112015014153A2/pt
Publication of WO2014097799A1 publication Critical patent/WO2014097799A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials

Definitions

  • the present invention relates to a method for hydrolyzing plant biomass. More specifically, the present invention relates to a hydrolysis method capable of obtaining a high glucose yield in which a reaction inhibition factor of hydrolysis by hydrothermal treatment of plant biomass is eliminated.
  • Patent Document 1 describes a method of hydrolyzing cellulose powder by contacting it with pressurized hot water heated to 200 to 300 ° C. (hydrolysis method by hydrothermal treatment).
  • Patent Document 2 describes a method in which an activated carbon solid acid catalyst treated with sulfuric acid is used as a solid catalyst for hydrothermal reaction.
  • Patent Document 3 discloses a method for obtaining a glucose yield of 60% or more by bringing a raw material containing cellulose and an aqueous solution containing an inorganic acid into contact with each other and subjecting the mixture to heat and pressure treatment.
  • JP 2011-206044 A discloses a method for obtaining a glucose yield of 60% or more by bringing a raw material containing cellulose and an aqueous solution containing an inorganic acid into contact with each other and subjecting the mixture to heat and pressure treatment.
  • An object of the present invention is to provide a method for obtaining a high glucose yield by eliminating a reaction inhibition factor in a method for hydrolyzing plant biomass.
  • the present inventors have intensively studied to solve the above problems. As a result, in the hydrolysis of plant biomass by hydrothermal treatment, by adding an acid according to the equivalent concentration of hydroxide ions and cations in the reaction solution, the reaction inhibition factor is released and a high glucose yield can be obtained. As a result, the present invention has been completed.
  • the present invention provides the following plant biomass hydrolysis method [1] to [7] and glucose production method [8].
  • Hydrothermal treatment is performed by adding an acid having an equivalent concentration of 30 to 1000% of the equivalent concentration of cations in the hydrolysis reaction solution of plant biomass and the equivalent concentration of hydroxide ions to the reaction solution.
  • a method for hydrolyzing plant biomass characterized by the above.
  • [2] The method for hydrolyzing plant biomass according to item 1 above, wherein a solid catalyst is used for the hydrothermal treatment.
  • the method for hydrolyzing plant biomass according to item 1 or 2 wherein the acid is at least one selected from inorganic mineral acids, organic carboxylic acids, and organic sulfonic acids
  • the cation in the reaction solution is 4.
  • hydrothermal treatment is performed by adding an acid to an equivalent concentration of 30 to 1000% of the equivalent concentration of the cation contained in the reaction solution.
  • a method for producing glucose wherein the method for hydrolyzing plant biomass according to any one of items 1 to 7 above is used.
  • reaction inhibition factors such as hydroxide ions and cations in the hydrolysis reaction solution are released, and a high glucose yield can be obtained.
  • Example 3 shows a comparison of the product yield when sulfuric acid is added before the reaction using dehydrated dry bagasse (Example 2).
  • the method for hydrolyzing plant biomass of the present invention is characterized in that the reaction inhibition of hydroxide ions and cations is canceled by allowing a specific amount of acid to coexist in the reaction solution.
  • Plant biomass generally refers to “renewable biological organic resources excluding fossil resources”.
  • plant biomass means mainly cellulose such as rice straw, straw, sugar cane leaf, rice husk, bagasse, hardwood, bamboo, conifer, kenaf, furniture waste wood, building waste wood, waste paper, food residue, etc.
  • plant biomass is used as a solid substrate for the hydrolysis reaction.
  • Plant biomass can be used as it is as a solid substrate, but pretreatments such as alkali cooking, alkaline sulfite cooking, neutral sulfite cooking, alkaline sodium sulfide cooking, ammonia cooking, sulfuric acid cooking, hydrothermal cooking, etc. Later, a residue that has been subjected to operations such as neutralization, water washing, dehydration, and drying to reduce the content of lignin and hemicellulose, and containing two or more of cellulose, hemicellulose, and lignin, Industrially prepared cellulose, xylan, cellooligosaccharide, xylooligosaccharide, and the like can be used.
  • plant biomass may be dry or wet and may be crystalline or non-crystalline.
  • the particle size of the plant biomass is not limited as long as it can be pulverized, but it is preferably 20 ⁇ m or more and several thousand ⁇ m or less from the viewpoint of pulverization efficiency.
  • Solid catalyst In the hydrolysis method by hydrothermal treatment of the present invention, a solid catalyst can also be used.
  • the solid catalyst is not particularly limited as long as it is a catalyst capable of hydrolyzing plant biomass polysaccharides. For example, it is represented by ⁇ -1,4 glycosidic bond between glucose forming cellulose as a main component. It preferably has an activity of hydrolyzing glycosidic bonds.
  • the solid catalyst for example, carbon materials and transition metals can be used alone or in combination of two or more.
  • the carbon material for example, activated carbon, carbon black, graphite and the like can be used alone or in combination of two or more.
  • the shape of the carbon material is preferably porous and / or fine particles in terms of improving reactivity by expanding the contact area with the substrate, and in terms of promoting acid hydrolysis by expressing acid sites. It preferably has a surface functional group such as a phenolic hydroxyl group, a carboxyl group, a sulfonyl group, or a phosphate group.
  • Porous carbon materials possessing surface functional groups include woody materials such as palm, bamboo, pine, walnut, and bagasse, coke, and phenol at high temperatures using gases such as water vapor, carbon dioxide, and air.
  • activated carbon prepared by a chemical method such as a chemical method of treating at a high temperature using a chemical such as alkali or zinc chloride. Specifically, an alkali activated porous carbon material or the like can be used.
  • transition metal for example, one selected from the group consisting of ruthenium, platinum, rhodium, palladium, iridium, nickel, cobalt, iron, copper, silver and gold may be used alone or in combination of two or more. Also good. From the viewpoint of high catalytic activity, those selected from the platinum group metals of ruthenium, platinum, rhodium, palladium and iridium are preferred, and from the viewpoint of high cellulose conversion and glucose selectivity, they are selected from ruthenium, platinum, palladium and rhodium. Those are particularly preferred.
  • Cellulose which is the main component of polysaccharides contained in plant biomass, exhibits crystallinity by binding two or more cellulose molecules by hydrogen bonding.
  • cellulose having such crystallinity can be used as a raw material, but cellulose having crystallinity lowered by a treatment for lowering crystallinity can also be used.
  • Cellulose with reduced crystallinity can be partially reduced in crystallinity, or completely or almost completely lost.
  • the type of the crystallinity reduction treatment is not particularly limited, but is preferably a crystallinity reduction treatment that can break the hydrogen bond and at least partially generate a single-chain cellulose molecule.
  • Examples of a method for breaking hydrogen bonds between cellulose molecules include pulverization.
  • the pulverizing means is not particularly limited as long as it has a function capable of being pulverized.
  • the system of the apparatus may be either dry or wet, and the grinding system of the apparatus may be either batch or continuous.
  • pulverization force such as an impact, compression, shear, friction, can be used.
  • Specific devices include rolling ball mills such as pot mills, tube mills, and conical mills, vibration ball mills such as circular vibration type vibration mills, swivel type vibration mills, and centrifugal mills, stirring tank mills, annular mills, flow type mills, and tower type grinding.
  • rolling ball mills such as pot mills, tube mills, and conical mills
  • vibration ball mills such as circular vibration type vibration mills, swivel type vibration mills, and centrifugal mills
  • stirring tank mills such as annular mills, flow type mills, and tower type grinding.
  • Agitator mills swirl type jet mills, impingement type jet mills, fluidized bed type jet mills, wet type jet mills, etc., jet mills, roughing machines (crushers), shear mills such as ong mills, mortars, Impact type crushers such as colloid mills such as stone mills, hammer mills, cage mills, pin mills, disintegrators, screen mills, turbo type mills, centrifugal classification mills, and planetary pulverizers that employ rotation and revolving motions. Examples include a ball mill.
  • the pulverizer is preferably a rolling ball mill, a vibrating ball mill, a stirring mill, or a planetary ball mill, which is used for pretreatment for reducing the crystallinity of the substrate, and is classified as a pot mill or stirring mill classified as a rolling ball mill.
  • the ratio of the solid catalyst and the solid substrate to be simultaneously pulverized is not particularly limited, but from the viewpoint of hydrolysis efficiency during the reaction, reduction of the substrate residue after the reaction, and recovery rate of the produced sugar,
  • the mass ratio is preferably 1: 100 to 1: 1, and more preferably 1:10 to 1: 1.
  • the raw material obtained by individually pulverizing the substrate and the raw material obtained by simultaneously pulverizing the substrate and the catalyst were both determined as the average particle size after pulverization (cumulative median diameter (median diameter): 100% of the total volume of the powder group. From the viewpoint of improving the reactivity, the particle diameter at the point where the cumulative curve becomes 50% is preferably 1 to 100 ⁇ m, more preferably 1 to 30 ⁇ m.
  • a rougher such as a shredder, jaw crusher, gyratory crusher, cone crusher, hammer crusher, roll crusher, roll mill, etc.
  • Preliminary pulverization can be performed using a pulverizer and a medium pulverizer such as a stamp mill, an edge runner, a cutting / shearing mill, a rod mill, an autogenous pulverizer, and a roller mill.
  • a medium pulverizer such as a stamp mill, an edge runner, a cutting / shearing mill, a rod mill, an autogenous pulverizer, and a roller mill.
  • the processing time of a raw material will not be limited if the raw material after a process is pulverized uniformly.
  • the hydroxide ions in the reaction solution are generally derived from the alkali chemicals used for the pretreatment of the hydrolysis reaction of the plant biomass that is the raw material.
  • the equivalent concentration of hydroxide ions in the reaction solution can be determined from the measured pH by the following formula.
  • the cation in the reaction solution refers to alkali metal ions and alkaline earths derived from plant biomass and solid catalyst as raw materials and / or derived from alkali chemicals used for the pretreatment of the hydrolysis reaction.
  • the equivalent concentration of cations in the reaction solution is determined by ion chromatography analysis, indophenol blue absorptiometry, ICP (inductively coupled plasma), EPMA (electron beam microanalyzer), ESCA (X-ray photoelectron spectrometer), SIMS (secondary ion). Mass spectrometry), atomic absorption method and the like can be obtained by summing up the results. It is preferable to use ion chromatographic analysis from the viewpoint that the main cations in the reaction solution can be directly measured with high sensitivity.
  • Acids include inorganic mineral acids such as hydrochloric acid, sulfuric acid, nitric acid and phosphoric acid, organic carboxylic acids such as acetic acid, formic acid, phthalic acid, lactic acid, malic acid, fumaric acid, citric acid and succinic acid, methanesulfonic acid and ethanesulfone Acid, organic sulfonic acid such as benzenesulfonic acid, toluenesulfonic acid and the like can be used alone or in combination of two or more.
  • inorganic mineral acids such as hydrochloric acid, sulfuric acid, nitric acid and phosphoric acid
  • organic carboxylic acids such as acetic acid, formic acid, phthalic acid, lactic acid, malic acid, fumaric acid, citric acid and succinic acid, methanesulfonic acid and ethanesulfone Acid
  • organic sulfonic acid such as benzenesulfonic acid, toluen
  • inorganic mineral acids are preferable, and sulfuric acid, hydrochloric acid, and nitric acid are more preferable from the viewpoint that the acid itself is not easily decomposed and denatured during hydrothermal treatment, and the inhibitory property when using the target product sugar is low. .
  • the lower limit value of the acid concentration can be set from the viewpoint of recovering the glucose saccharification rate to a higher level, and the upper limit value can be set from the viewpoint of suppressing the excessive decomposition of glucose and suppressing the corrosiveness by the acid.
  • the acid is preferably present in the reaction solution at an equivalent concentration in the range of 30 to 1000% of the equivalent concentration of the cation in the reaction solution, more preferably in the range of 50 to 500%. More preferably, an equivalent concentration in the range of ⁇ 300% is present. Therefore, when hydroxide ions are present in the reaction solution before the acid is added, it is necessary to add an acid having a total equivalent concentration obtained by adding the equivalent concentration of hydroxide ions to the equivalent concentration in the above range. This is because the presence of hydroxide ions consumes the acid by neutralization.
  • Hydrolysis using plant biomass as a substrate is performed by hydrothermal treatment.
  • the hydrothermal treatment is carried out by heating the substrate in the presence of water, preferably adding a solid catalyst, and heating at a temperature at which the substrate is pressurized.
  • the temperature for heating to be in a pressurized state is suitably in the range of 110 to 380 ° C., from the viewpoint of rapidly hydrolyzing cellulose and suppressing the conversion of the product glucose to other sugars.
  • a relatively high temperature is preferable, for example, a temperature in the range of 170 to 320 ° C., more preferably 180 to 300 ° C. is appropriate.
  • the hydrothermal treatment in the hydrolysis method of the present invention is usually carried out in a closed container such as an autoclave, even if the reaction is started at normal pressure, if the reaction system is heated at the above temperature, Become. Further, the reaction can be carried out by pressurizing the inside of the sealed container before or during the reaction.
  • the pressure to be applied is, for example, 0.1 to 30 MPa, preferably 1 to 20 MPa, and more preferably 2 to 10 MPa.
  • the reaction can also be carried out by heating and pressurizing the reaction solution with a high-pressure pump.
  • the amount of water for hydrolysis is an amount capable of hydrolyzing at least cellulose and hemicellulose in the plant biomass, and considering the fluidity and agitation of the reaction mixture,
  • the mass ratio is preferably in the range of 1 to 500, more preferably in the range of 2 to 200.
  • the atmosphere for the hydrolysis is not particularly limited. Industrially, it is preferably performed in an air atmosphere, but may be performed in an atmosphere of a gas other than air, for example, oxygen, nitrogen, hydrogen, or a mixture thereof.
  • the heating of the hydrothermal treatment is terminated when the conversion rate by hydrolysis of cellulose is between 10 and 100% and the selectivity of glucose is between 20 and 80%. Is preferable.
  • the heating time is in the range of 5 to 60 minutes, preferably 5 to 30 minutes from the start of heating for the hydrolysis reaction under normal conditions, but is not limited to this range.
  • the heating for hydrolysis is such that the conversion by hydrolysis of cellulose is preferably in the range of 30 to 100%, more preferably in the range of 40 to 100%, still more preferably in the range of 50 to 100%, most preferably. Is in the range of 55-100% and ends when the glucose selectivity is preferably in the range of 25-80%, more preferably in the range of 30-80%, most preferably in the range of 40-80%. Is appropriate.
  • the form of the hydrolysis reaction may be either a batch type or a continuous type.
  • the reaction is preferably carried out while stirring the reaction mixture.
  • it is possible to produce a sugar-containing liquid containing glucose as a main component and containing a small amount of a hyperdegradation product such as 5-hydroxymethylfurfural by a hydrolysis reaction at a relatively high temperature for a relatively short time.
  • the reaction solution After completion of heating, it is preferable to cool the reaction solution from the viewpoint of suppressing the conversion of glucose to other sugars and increasing the glucose yield. From the viewpoint of increasing the glucose yield, the reaction solution is preferably cooled under the condition that the selectivity of glucose is maintained in the range of 20 to 80%, more preferably in the range of 25 to 80%, and 30 to 80%. Is more preferable, and the range of 40 to 80% is most preferable.
  • the reaction solution is preferably cooled as quickly as possible to a temperature at which the conversion of glucose into other sugars does not occur, for example, at a rate in the range of 1 to 200 ° C./min.
  • the rate is preferably in the range of 5 to 150 ° C./min.
  • the temperature at which the conversion of glucose into other sugars does not occur is, for example, 150 ° C. or lower, preferably 110 ° C. or lower. That is, the reaction solution is suitably cooled to a temperature of 150 ° C. or lower at a rate of 1 to 200 ° C./min, preferably 5 to 150 ° C./min.
  • the obtained reaction liquid can be separated and recovered into a liquid phase containing glucose and a solid phase containing a solid catalyst and an unreacted substrate by solid-liquid separation treatment.
  • a centrifuge, a centrifugal filter, a pressure filter, a Nutsche filter, or a filter press can be used for solid-liquid separation, but it is limited as long as the liquid phase and the solid phase can be separated. It is not something.
  • Coke (coal coke, manufactured by Showa Denko KK) was heat-treated at 700 ° C and finely pulverized with a jet mill, and then potassium hydroxide was added and heat-treated again at 700 ° C to activate.
  • the obtained activated coke is washed with water, neutralized with hydrochloric acid, boiled with hot water, dried, and sieved to obtain an alkali-activated porous carbon material having a particle size of 1 ⁇ m to 30 ⁇ m (median diameter 13 ⁇ m). (Hereinafter referred to as a carbon catalyst).
  • centrifugal filter manufactured by Kokusan Co., Ltd. 1000 g of water-containing solid content (water content 70%, dry product equivalent 300 g) from which the supernatant was removed by H-110A) was recovered.
  • Washing pretreatment bagasse 10.00 g as a solid substrate and carbon catalyst 1.54 g (substrate to catalyst mass ratio 6.5: 1.0) were placed in an alumina sphere having a diameter of 1.5 cm in a ceramic pot mill with a capacity of 3600 mL. Added with 2000 g.
  • This ceramic pot mill was set on a desktop pot mill rotary table (manufactured by Nissho Scientific Co., Ltd., desktop pot mill model ANZ-51S), and ball milled at 60 rpm for 48 hours to mix and grind simultaneously.
  • the obtained raw material is referred to as a cleaning mixed pulverized raw material.
  • the reaction solution After cooling, the reaction solution is separated into a liquid and a solid by a centrifugal separator, and the product in the liquid phase is a high performance liquid chromatograph (device: Shodex high performance liquid chromatography manufactured by Showa Denko KK, column: Shodex (registered trademark)).
  • KS801 mobile phase: water 0.6 mL / min, 75 ° C., detection: differential refractive index).
  • the cellulose conversion rate was calculated
  • PH measurement The pH was measured at 25 ° C. in a glass bottle using a pH meter D-51 (manufactured by Horiba, Ltd.) calibrated at three points using Horiba Seisakusho pH STANDARD 100-4, 100-7, and 100-9. After immersing the glass electrode of the device in the solution, the mixture was lightly stirred and then allowed to stand and measured until it became stable (about 1 minute).
  • Reference Example 1, Example 1 and Comparative Examples 1 to 2 Solid catalyst addition desensitized individually pulverized starting material 0.324g by reaction inhibition and acid by the hydroxide ions and cations in the reaction (C 6 H 10 O 5 units 2. 00 mmol) and 0.050 g of a solid catalyst, 40 mL of an aqueous dispersion prepared by adjusting the inhibitor (NaOH) and acid (H 2 SO 4 ) shown in Table 1 so as to have the equivalent concentration shown in Table 1. The mixture was placed in a high-pressure reactor (internal volume: 100 mL, autoclave manufactured by OM Labtech Co., Ltd., Hastelloy (registered trademark) C22), and heated from room temperature to a reaction temperature of 200 ° C.
  • a high-pressure reactor internal volume: 100 mL, autoclave manufactured by OM Labtech Co., Ltd., Hastelloy (registered trademark) C22
  • Example 1 in which the amount of sulfuric acid minus the neutralization content is 90% of the relative ratio to the equivalent concentration of the cation exhibits the effect of releasing the inhibition and recovers to the same level of saccharification results as in Reference Example 1. (Fig. 1).
  • the reaction inhibition factor is eliminated by a simple method in which an acid is allowed to coexist depending on the equivalent concentration of hydroxide ions and cations in the reaction solution. Yields can be obtained.

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Abstract

Cette invention concerne un procédé d'hydrolyse d'une biomasse végétale qui consiste à ajouter une concentration équivalente d'acide égale à la concentration équivalente d'ions hydroxyde dans une solution de réaction d'hydrolyse d'une biomasse végétale plus 30 à 1000 % de la concentration équivalente de cations qu'elle contient et à procéder à un traitement hydrothermique. Cette invention concerne également un procédé de production de glucose faisant appel au procédé d'hydrolyse précité. Le traitement hydrothermique précité est de préférence mis en œuvre à l'aide d'un acide inorganique à titre de l'acide précité et à l'aide d'un catalyseur solide comprenant une matière carbonée. La présente invention élimine les facteurs qui inhibent la réaction provenant des cations présents dans le système réactionnel, ce qui résulte en un rendement de glucose élevé.
PCT/JP2013/081181 2012-12-18 2013-11-19 Procédé d'hydrolyse d'une biomasse végétale WO2014097799A1 (fr)

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JP2014553028A JPWO2014097799A1 (ja) 2012-12-18 2013-11-19 植物性バイオマスの加水分解方法
US14/652,980 US20150337401A1 (en) 2012-12-18 2013-11-19 Plant-biomass hydrolysis method
BR112015014153A BR112015014153A2 (pt) 2012-12-18 2013-11-19 método de hidrólise de biomassa de planta

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JP2012275514 2012-12-18
JP2012-275514 2012-12-18

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CN111747410A (zh) * 2019-03-26 2020-10-09 天津科技大学 一种水热法制备汉麻秆芯基炭材料的方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10327900A (ja) * 1997-06-02 1998-12-15 Agency Of Ind Science & Technol 水溶性オリゴ糖類及び単糖類の製造方法
JP2009201405A (ja) * 2008-02-27 2009-09-10 Kochi Univ グルコースの製造方法およびスルホン化活性炭の製造方法
WO2011036955A1 (fr) * 2009-09-25 2011-03-31 国立大学法人北海道大学 Catalyseur pour l'hydrolyse de la cellulose ou de l'hémicellulose, et procédé de production d'une solution contenant un sucre à l'aide dudit catalyseur
JP2011142894A (ja) * 2010-01-18 2011-07-28 Ihi Corp バイオマス処理装置
JP2011206044A (ja) * 2009-09-30 2011-10-20 Sekisui Chem Co Ltd セルロース糖化方法
JP2011217634A (ja) * 2010-04-06 2011-11-04 Toyota Motor Corp 植物バイオマスの処理方法、植物バイオマスからの糖の製造方法、植物バイオマスからのアルコール及び／又は有機酸の製造方法
JP2012000022A (ja) * 2010-06-15 2012-01-05 Tsukishima Kikai Co Ltd バイオマスの処理装置及び処理方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7503981B2 (en) * 2004-12-02 2009-03-17 The Trustees Of Dartmouth College Removal of minerals from cellulosic biomass
CA2644074A1 (fr) * 2006-03-01 2007-09-07 National University Corporation Hokkaido University Catalyseur d'hydrolyse de cellulose et/ou de reduction du produit d'hydrolyse et procede de production d'un alcool sucre a partir de la cellulose
JP4765073B2 (ja) * 2006-07-05 2011-09-07 国立大学法人広島大学 リグノセルロースの水熱加水分解方法
JP2011103874A (ja) * 2009-10-22 2011-06-02 Idemitsu Kosan Co Ltd バイオマスの処理方法
JP2011101608A (ja) * 2009-11-10 2011-05-26 Ihi Corp バイオマス処理システム及び方法
AR081449A1 (es) * 2010-04-07 2012-09-05 Licella Pty Ltd Metodos para produccion de biocombustibles
US9109049B2 (en) * 2012-06-21 2015-08-18 Iowa State University Research Foundation, Inc. Method for pretreating lignocellulosic biomass

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10327900A (ja) * 1997-06-02 1998-12-15 Agency Of Ind Science & Technol 水溶性オリゴ糖類及び単糖類の製造方法
JP2009201405A (ja) * 2008-02-27 2009-09-10 Kochi Univ グルコースの製造方法およびスルホン化活性炭の製造方法
WO2011036955A1 (fr) * 2009-09-25 2011-03-31 国立大学法人北海道大学 Catalyseur pour l'hydrolyse de la cellulose ou de l'hémicellulose, et procédé de production d'une solution contenant un sucre à l'aide dudit catalyseur
JP2011206044A (ja) * 2009-09-30 2011-10-20 Sekisui Chem Co Ltd セルロース糖化方法
JP2011142894A (ja) * 2010-01-18 2011-07-28 Ihi Corp バイオマス処理装置
JP2011217634A (ja) * 2010-04-06 2011-11-04 Toyota Motor Corp 植物バイオマスの処理方法、植物バイオマスからの糖の製造方法、植物バイオマスからのアルコール及び／又は有機酸の製造方法
JP2012000022A (ja) * 2010-06-15 2012-01-05 Tsukishima Kikai Co Ltd バイオマスの処理装置及び処理方法

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